EP0643678B1 - Production d'ethyltoluene - Google Patents

Production d'ethyltoluene Download PDF

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Publication number
EP0643678B1
EP0643678B1 EP93915202A EP93915202A EP0643678B1 EP 0643678 B1 EP0643678 B1 EP 0643678B1 EP 93915202 A EP93915202 A EP 93915202A EP 93915202 A EP93915202 A EP 93915202A EP 0643678 B1 EP0643678 B1 EP 0643678B1
Authority
EP
European Patent Office
Prior art keywords
isomer
ethyltoluene
catalyst
toluene
ortho
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP93915202A
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German (de)
English (en)
Other versions
EP0643678A4 (en
EP0643678A1 (fr
Inventor
Cynthia Ting-Wah Chu
Yun Yang Huang
Donald J. Klocke
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Oil Corp
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Mobil Oil Corp
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Publication of EP0643678A1 publication Critical patent/EP0643678A1/fr
Publication of EP0643678A4 publication Critical patent/EP0643678A4/en
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
    • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
    • C07C2/66—Catalytic processes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • This invention relates to a process for the production of ethyltoluene and more particularly, to a process for the production of a mixture of ethyltoluene isomers having a high content of the meta isomer and a very low quantity of the ortho isomer.
  • Vinyl toluene is an important industrial commodity chemical used for the production of polymers. For certain purposes, it is desirable to produce vinyl toluene with a relatively high content of the meta isomer (m-methyl styrene), typically from 50 to 70% of the total vinyl toluene content. At the same time, a very low content of the ortho isomer (o-methyl styrene) is desired since this material acts as a chain stopper in polymerization. Normally, a maximum content of the ortho isomer of 1.5% and preferably below 1 or 0.5% must be adhered to for a commercially acceptable material.
  • m-methyl styrene meta isomer
  • o-methyl styrene o-methyl styrene
  • Vinyl toluene is produced from ethyltoluene by dehydrogenation with the isomer ratio of the vinyl toluene product being directly dependent upon the isomer ratio of the ethyltoluene precursor.
  • the ethyltoluene should typically contain from 50 to 70% of the meta isomer and not more than 1% ortho isomer with the balance being made up of the para isomer.
  • Ethyltoluene may be produced by the ethylation of toluene in the presence of an acidic catalyst and for this purpose, Lewis acid type catalysts such as aluminum chloride as well as heterogeneous zeolite catalyst have been used. Homogenous phase Lewis acid catalysts such as aluminum trichloride are effective for the ethylation of toluene under relatively mild conditions to produce an ethyltoluene product in which the isomer ratio is relatively close to the equilibrium ratio of 31.5% para, 50.2% meta and 18.3% ortho.
  • Lewis acid type catalysts such as aluminum chloride
  • heterogeneous zeolite catalyst heterogeneous zeolite catalyst
  • Example 13 discloses (Example 13) a process in which toluene is ethylated in the presence of aluminum chloride to produce ethyltoluene with a p-:m-:o- isomer ratio of 27:60:13. While this ethyltoluene product has the requisite content of the meta isomer, the ortho isomer is present in excessive amounts.
  • An intermediate pore size zeolite such as ZSM-5 may be used to catalyze the ethylation of toluene, typically using temperatures in the range of 260° to 455°C (500° to 850°F).
  • the isomer ratio of the product varies according to the specific shape selectivity characteristics of the zeolite component of the catalyst. If ZSM-5 is used in its hydrogen form without modification, the ethyltoluene product has an isomer ratio which is relatively close to equilibrium. An example of this is given in US 4086287 where Example 3 shows that a meta content of about 60% may be obtained but that the ortho isomer is present in excessive amounts.
  • the alpha value of the catalyst in US 4086287 is preferably less than 20, and this may be obtained by steaming.
  • the content of the ortho isomer may be reduced to suitably low levels but this is accompanied by a major increase in the selectivity to the para isomer to the extent that the process is highly regioselective.
  • ZSM-5 is modified with magnesium, phosphorous or boron
  • the content of the ortho isomer may be reduced almost to zero but in this case, selectivity for the para isomer is exceptionally high so that the ethyltoluene product does not have the desired balance of the para and meta isomer components. Processes such as this are described in U. S. Patents No. 4,086,287 and 4,143,084.
  • U.S. Patent No. 4,489,214 discloses a process for producing ethyltoluene using a catalytic material described as "silicalite", a material known to be a highly siliceous from of zeolite ZSM-5. See Fyfe et al., "Resolving crystallographically distinct sites in silicalite and ZSM-5 by soid state NMR", Nature 296 , 530 (1982) and Olson, D. H. et al., J. Catalysis 61 , 390-396 (1980).
  • the problem remains of producing ethyltoluene with a relatively high content of the meta isomer and a low content of the ortho isomer not exceeding 1.5% and preferably less than 0.5%.
  • m-:p- ratio of the product is at least 1:1 (m-:p-) and preferably at least 1.5:1 by weight; the level of the ortho isomer does not, in any event, exceed 1.5% and is usually below 1%.
  • the ethyltoluene product is produced by the ethylation of toluene in the presence of an intermediate pore size aluminosilicate zeolite catalyst of controlled acidity produced by steaming.
  • the reaction is carried out at temperatures from 370° to 480°C (700° to 900 °F) with toluene:ethylene ratios from 2:1 to 20:1 and space velocities based on the toluene feed, of 10 to 40 (WHSV).
  • the temperature will normally not exceed 455°C (850°F).
  • toluene is reacted with ethylene in the presence of an intermediate pore size steamed aluminosilicate zeolite catalyst.
  • the objective is to produce an ethyltoluene product which has a high content of the meta isomer and a very low content of the ortho isomer.
  • the meta: para ratio of the product is at least 1:1 by weight (equivalent to at least 50 weight percent of the meta-isomer on an ortho-free basis) and is preferably at least 1.2:1 (at least 55 weight percent meta- on an ortho-free basis).
  • the maximum content of the ortho isomer is to be maintained at 1.5% and should preferably be below 1% or, better, 0.5% by weight if the ethyltoluene product is to be used for a polymerization grade vinyltoluene.
  • the activity and selectivity of the catalyst are modified together and used in combination with selected reaction parameter to produce an ethyltoluene product with the required isomer distribution.
  • the proportion of ethylbenzene by-product, produced by disproportionation of the toluene feed is minimized by controlling the activity of the catalyst to inhibit the disproportionation reaction while maintaining a sufficient contact time (reciprocal space velocity) to shift the composition of the desired ethyltoluene product to the desired isomer distribution.
  • the catalyst includes aluminosilicate zeolite ZSM-5 as the essential catalytic component.
  • This zeolite an intermediate pore size zeolite, is matrixed with a binder such as alumina in order to give sufficient strength to the catalyst and in order to avoid binder effects a low acidity material is preferred.
  • the ZSM-5 should have a crystallite size of at least one micron in order to provide the desired diffusion characteristics and crystallite sizes of about 1.5 microns or more e.g. 2 micron are preferred. ZSM-5 with this crystal size may be readily made by conventional techniques using substituted ammonium directing agents such as tetrapropylammonium cations in combination with trimethylammonium cations, as described in U.S. 4,375,458 (Dwyer) to which reference is made for a description of such a technique.
  • Activity of the zeolite is maintained at a controlled, relatively low level, by steaming the original zeolite in order to reduce the incidence of side reactions such as the toluene disproportionation reaction.
  • the acid activity of the catalyst should be maintained at an alpha value of not more than 80, preferably not greater than 50, more preferably not greater than 40. It has been found that an alpha value of about 30 gives good results.
  • the alpha value is an approximate indication of the catalytic cracking activity of the catalyst compared to a standard catalyst.
  • the alpha test is described in U.S. Patent 3,354,078 and in J. Catalysis , 4 , 527 (1965); 6 , 278 (1966); and 61 , 395 (1980), to which reference is made for a description of the test.
  • the experimental conditions of the test used to determine the alpha values referred to in this specification include a constant temperature of 538°C and a variable flow rate as described in detail in J. Catalysis , 61 , 395 (1980).
  • the reaction is carried out by passing toluene and ethylene together over the ZSM-5 catalyst at temperatures in the range of about 260° to 455°C (about 500° to about 850°F).
  • the contact time (reciprocal space velocity) is maintained at a value which enables the product composition to shift sufficiently to give the desired content of the meta isomer while maintaining the ortho content at the necessary low level.
  • reaction temperature and contact time are both related to total reaction severity, a trade off may be affected between temperature and space velocity with decreasing space velocity increasing the content of the meta and ortho isomers.
  • temperatures will be from about 400° to 455°C about 750° to 850°F with space velocities, based on the toluene feed, from 10 to 40 WHSV.
  • the relatively high velocities are important. In a commercial process, high space velocities enable more product to be produced in a unit of a given size. Additionally, we discovered that the space velocity contributes to a product mixture that contains high amounts of the meta-isomer and only minimal amounts of the ortho-isomer.
  • reaction is not critical with respect to pressure and for reasons of economy it will be convenient to operate at low to moderate pressures, typically up to about 3550 kPa abs about 500 psig although higher pressures may be used if desired.
  • a relatively high ratio of toluene to ethylene is preferred in order to ensure a high selectivity of ethylene to ethyltoluene.
  • the ratio of toluene to ethylene will be from 2:1 to about 30:1 and in most cases ratios from 10:1 to 20:1 (molar) will be satisfactory.
  • Catalyst A is not in accordance with the invention. It provides a comparative example. Toluene and ethylene were passed over the catalysts at temperatures from 432° to 446°C (810° to 835°F) at a pressure of 1130 kPa abs (150 psig). The space velocity based on the toluene feed was 130 WHSV. A toluene: ethylene mole ratio of 16 was employed. The results are given in Table 1 below.
  • reaction severity contact time, temperature
  • Toluene ethylation was carried out at temperatures from 404 to 421 °C (760° to about 790°F) (reactor inlet). Space velocity based on the toluene feed varied from 20 to 130 (WHSV).
  • a toluene:ethylene mole ratio of 7 or 16 was used at a pressure of 1.13 mPa (150 psig). No hydrogen was added.
  • Table 2 Ethyltoluene Production - Reaction Severity TOS, hr 26 2 6 9 Temp.
  • the effect of the ZSM-5 crystal size was investigated with two ZSM-5 catalysts.
  • the first catalyst (Catalyst D) had an alpha value of 50 and a zeolite crystal size of less than 0.05 ⁇ m and the second (Catalyst E) an alpha value of 18 and a crystal size between 0.1 and 1 ⁇ m.
  • the two catalysts were used to ethylate toluene at temperatures from about 415 to 460°C (about 780° to 860°F) in the absence of hydrogen at a pressure of 1135 kPaa (150 psig).
  • the results for Catalyst D are given in Table 5 and for Catalyst E in Table 6 below.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

L'éthyltoluène est produit par éthylation de toluène en présence d'un catalyseur ZSM-5 ayant une acidité et un pouvoir de diffusion régulés afin de produire un mélange d'isomère d'éthyltoluène dont la concentration d'isomère méta est élevée et dont la concentration d'isomère ortho est très faible. Le rapport pondéré entre l'isomère méta et le isomère para est d'au moins 1:1, de préférence 1,2:1, tandis que l'isomère ortho est maintenu sous 1,5 %, de préférence en-dessous de 0,5 %. L'éthyltoluène produit peut être déshydrogéné afin de former le toluène de vinyle de qualité polymérisation.

Claims (8)

  1. Un procédé de fabrication d'un mélange d'isomèreS d'éthyltoluène à haute teneur en isomère meta- et à très faible teneur en isomère ortho-, qui comprend l'éthylation du toluène par l'éthylène en présence d'un catalyseur comprenant une ZSM-5 présentant une dimension de cristallite d'au moins un micron et qui a été traitée à la vapeur d'eau pour lui conférer une valeur de alpha ne dépassant 80, à une température de 370 à 480°C (700 à 900°F) et à une vitesse spatiale, exprimée par rapport à la charge de toluène, comprise entre 10 et 40 WHSV, pour obtenir un produit réactionnel comprenant un mélange d'isomères de l'éthyltoluène dans lequel le rapport pondéral de l'isomère méta- à l'isomère para- est d'au moins 1/1 et de moins de 1,5 % en poids d'isomère ortho-.
  2. Un procédé selon la revendication 1, dans lequel le rapport pondéral de l'isomère méta- à l'isomère para- dans le mélange d'isomères d'éthyltoluène est d'au moins 1,2/1.
  3. Un procédé selon la revendication 1, dans lequel la teneur en isomère ortho- du mélange d'isomères d'éthyltoluène n'est pas supérieure à 1 % en poids.
  4. Un procédé selon la revendication 1, dans lequel la teneur en isomère ortho- dans le mélange d'isomères d'éthyltoluène n'est pas supérieure à 0,5 % en poids.
  5. Un procédé selon la revendication 1, dans lequel la dimension des cristallites de la ZSM-5 est d'au moins 2 microns.
  6. Un procédé selon la revendication 1, dans lequel le catalyseur a une valeur de alpha non supérieure à 50.
  7. Un procédé selon la revendication 5, dans lequel le catalyseur présente une valeur de alpha non supérieure à 40.
  8. Un procédé selon la revendication 1, dans lequel on fait réagir le toluène avec l'éthylène à une température comprise entre 399 et 480°C (750 à 850°F).
EP93915202A 1992-06-05 1993-06-03 Production d'ethyltoluene Expired - Lifetime EP0643678B1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US89448192A 1992-06-05 1992-06-05
US894481 1992-06-05
PCT/US1993/005319 WO1993025502A1 (fr) 1992-06-05 1993-06-03 Production d'ethyltoluene
CN93108930A CN1043223C (zh) 1992-06-05 1993-06-15 乙基甲苯的制备

Publications (3)

Publication Number Publication Date
EP0643678A1 EP0643678A1 (fr) 1995-03-22
EP0643678A4 EP0643678A4 (en) 1995-04-05
EP0643678B1 true EP0643678B1 (fr) 1997-02-12

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Application Number Title Priority Date Filing Date
EP93915202A Expired - Lifetime EP0643678B1 (fr) 1992-06-05 1993-06-03 Production d'ethyltoluene

Country Status (9)

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EP (1) EP0643678B1 (fr)
JP (1) JPH07507562A (fr)
CN (1) CN1043223C (fr)
AU (1) AU661189B2 (fr)
CA (1) CA2132532A1 (fr)
DE (1) DE69308133T2 (fr)
ES (1) ES2100547T3 (fr)
SG (1) SG42961A1 (fr)
WO (1) WO1993025502A1 (fr)

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4143084A (en) * 1976-07-19 1979-03-06 Mobil Oil Corporation Di-alkylbenzene isomer mixtures
US4086287A (en) * 1976-07-19 1978-04-25 Mobil Oil Corporation Selective ethylation of mono alkyl benzenes
US4104319A (en) * 1977-06-23 1978-08-01 Mobil Oil Corporation Ethylation of mono alkyl benzene
US4489214A (en) * 1982-03-01 1984-12-18 Cosden Technology, Inc. Production of ortho-suppressed dialkyl benzenes

Also Published As

Publication number Publication date
AU661189B2 (en) 1995-07-13
DE69308133T2 (de) 1997-05-28
EP0643678A4 (en) 1995-04-05
SG42961A1 (en) 1997-10-17
EP0643678A1 (fr) 1995-03-22
CN1096507A (zh) 1994-12-21
ES2100547T3 (es) 1997-06-16
DE69308133D1 (de) 1997-03-27
WO1993025502A1 (fr) 1993-12-23
CN1043223C (zh) 1999-05-05
AU4527593A (en) 1994-01-04
CA2132532A1 (fr) 1993-12-23
JPH07507562A (ja) 1995-08-24

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